1271217 經濟部智慧財產局員工消費合作社印製 A7 B7 五、發明說明（1) 本發明係關於催化反應器。 很多催化反應用布置於反應器之固定床顆粒催化劑進 行，一般爲圓形截面。工作流自入口通過固定床，並通過 出口流出反應益。$亥床通常布置成使工作氣流方向平行於 反應器轴。在此布置下，所稱軸向流（工作流體）一般向下 流動通過該床，使催化劑顆粒移動最小。該布置具有簡 單、易於填卸催化劑及使反應器内額外組分最小之優點。 因此，除非反應器中需要熱交換裝置，一般只須提供允許 流體通過之催化劑限制物，如適合大小之栅（板）或筛網， 以防止工作流體夾帶之催化劑顆粒通過工作氣體出口排 出0 爲使流體流動通過催化劑床，應在入口和出口之間建立 壓差。除其它外，所需壓差決於床厚度、床材料呈現之流 阻以及流體流動速率。通常理想使該壓差最小和/或在不 明顯增加所需壓差下增加流體流動速率。 爲此’有時採取更換布置（徑向流）之方法。因此，將顆 粒催化劑J還形布參，該環形由允許流禮通遷進催化 劑通過之構件界定（如於反應登直复，使工作流體自 反i器截面周邊周圍之入口區域徑向流動通過催化劑床， 進入於中心布置之出口區域。或者反向流動，即，自中心 入口區域徑向向外通過催化劑床，達到出口或於反應器周 邊布置之收集區域。亦可將徑向和軸向流組合使用。雖然 此類徑向流布置給予所需壓差優勢，使工作流體以理想速 率流動，但需要更複雜反應器内部，使顆粒催化劑加入和 -4- 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） ----------裝-----r--^丨訂 *-------- (請先閱讀背面之注意事項再填寫本頁) 1271217 Α7 Β7 五、發明說明（2 ) /或卸出不便。 我們設計出一種裝置，其中可獲得色^咸士垩差優曼坌提 、向u或轴向—徑向流’而沒有複雜反應内部之不利。 因此’本發明提供一種具入口和出口及顆粒催化劑床之 催化反應器，該催化劑床布置於連通一個口之中心區域周 圍，且比催化劑顆粒顯示更小流阻，該床内之中心區域至 少與該催化劑床之主要部分等高，對至少主要部分高度之 催化劑床而言，該催化劑床之外表面具小於反應器之截 面，因而在催化劑床外表面和反應器之内表面留下一個空 間。該2間用比催化劑顆粒顯示更小流阻之顆粒材料填 充。 該催化劑床較佳具有接近單個圓柱形或錐臺形之外表 面’考〜是.有一兩個ϋ個不同最大直徑圓柱或錐臺積形狀之 外表-面’或具有一或多個圓柱和一或多個錐臺堆積形狀之 ·*一一一’" 一 ...... 、 經濟部智慧財產局員工消費合作社印製 外表面。部分催化劑床可具有等於該反應器内徑之外徑， 即該部分在反應器内壁和催化劑床外表面之間沒有空間。 但該催化劑床外表面之最小外徑小於反應器之内徑，使至 少部分高度床在反應器内壁和催化劑床之外表面之間留有 S間。该2間用比該催化劑顆粒顯示小阻抗工作流體流動 之顆粒材料填充。 同樣，該催化劑床内之中心區域較佳具有接近圓錐、錐 臺或圓柱之形狀，或具有圓錐和一或多個錐臺或圓柱堆積 之形狀’或具有一或多個不同最大直徑圓柱或錐臺堆積之 形狀，或具有一或多個圓柱和一或多個錐臺堆積之形狀。 -5- 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） 1271217 A7 B7 經濟部智慧財產局員工消費合作社印製 五、發明說明（3 較佳具有接近單個圓柱或錐臺之形狀，較佳具有大於反應 器截面之表面積。催化劑床内中心區域之高度佔催化劑床 主要部分，較佳至少佔催化劑床高度7 〇 〇/〇。 本發明藉參考附圖説明，其中： 圖1爲根據本發明通過反應器布置軸向/徑向流之剖面 圖。 圖2爲類似圖1之另一個具體實施例視圖。 圖3至5爲圖1邵分反應器之部分剖面圖，用以説明加顆 粒材料至反應器之順序。 圖6爲類似圖1之另外一個具體實施例視圖。 圖1中顯示具圓柱截面之反應器1，該反應器1上端具有 入口 2 ’下端具有出口 3。催化劑限制穿孔裝置4 (例如圓 筒形線網籠）布置於出口 3上方，以界定自由空間5，形成 催化劑床内與出口 3連通之必要中心區域。在催化劑限制 裝置4周圍爲顆粒催化劑床，例如圓柱形顆粒。該催化劑 顆粒具有1至10毫米範圍之最大和最小尺寸以及1至5範圍 足長寬比（最大尺寸/最小尺寸）。催化劑限制裝置之孔隙 大小應使催化劑顆粒不能通過。反應器丨之内壁7和催化劑 床之外表面形成區域8，該區域8用比催化劑床6之顆粒顯 不更小流阻足顆粒材料填充。填充區域8之顆粒材料一般 具有大於催化劑顆粒之顆粒大小。此等顆粒之最小尺寸一 般爲催化劑顆粒最小尺寸之丨.5倍，最大尺寸較佳不大於 催化劑顆粒最大尺寸之2·5倍。此等較大顆粒可爲圓柱構 型，亦可具有一個或多個軸向延伸通孔，以降低工作流體 -----------裝---— III· — --- (請先閱讀背面之注意事項再填寫本頁) Φ -6 1271217 經濟部智慧財產局員JL消費合作社印製 A7 B7 五、發明說明（4) 通過區域8之流動阻力。區域8之顆粒亦可擴延到催化劑床 頂部9。 使用時，將工作流體送至入口 2，軸向向下流動通過區 域8，然後通過催化劑床6進入自由空間5，由此達到出口 3。由於區域8顯示流阻小於催化劑床6之流阻，所以工作 流體向下流動通過區域8，然後徑向通過催化劑床6，達到 自由空間5。同時，工作流體亦軸向向下流動通過高於催 化劑限制裝置4上部之部分催化劑床。如果催化劑限制裝 置4之頂部由固體製成，那麼可省略高於催化劑限制裝置4 頂部之催化劑床層，使通過催化劑床6之工作流體基本徑 向流動。或者，不管催化劑限制裝置4之頂部是否爲固 體’在^(隹化劑床頂部上安置圓盤或板，以改變通過催化劑 床較上部分之流動方式。 在圖2之具體貫施例中’催化劑限制裝置4以錐臺形式製 造，該催化劑床同樣爲常用臺錐構型。如此布置使得工作 流體通過催化劑床6之流動分布更加均勻。較佳將催化劑 限制裝置4布置成使工作流體通過催化劑床之流阻大體上 均勻。 圖3至5説明將顆粒材料填至反應器之方法。如圖3所 示’在反應器下壁1 1放置環1 〇，較佳在此位置於床6和區 域8之間形成接界，然後將催化劑顆粒填充至由催化劑p艮 制裝置4和環1 0包圍之環形區域。如圖4所示，用區域8所 需之顆粒填充環1 0和反應器壁7間之環形區域。如圖5所 示，提起環1 0，再放置於以前填充顆粒之上部，重複以上 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） -----------裝— (請先閱讀背面之注意事項再填寫本頁) 訂· 經濟部智慧財產局員工消費合作社印製 Α2712171271217 Ministry of Economic Affairs Intellectual Property Office Staff Consumer Cooperative Printed A7 B7 V. INSTRUCTIONS (1) The present invention relates to a catalytic reactor. Many catalytic reactions are carried out using fixed bed particulate catalysts disposed in the reactor, generally having a circular cross section. The workflow flows from the inlet through the fixed bed and out through the outlet. The hail bed is typically arranged such that the direction of the working gas flow is parallel to the reactor axis. In this arrangement, the so-called axial flow (working fluid) generally flows downwardly through the bed to minimize catalyst particle movement. This arrangement has the advantages of being simple, easy to load and unload the catalyst, and minimizing additional components in the reactor. Therefore, unless a heat exchange device is required in the reactor, it is generally only necessary to provide a catalyst limiter that allows the passage of fluid, such as a grid (plate) or screen of a suitable size, to prevent catalyst particles entrained by the working fluid from exiting through the working gas outlet. To allow fluid to flow through the catalyst bed, a pressure differential should be established between the inlet and the outlet. The required pressure differential depends, among other things, on the thickness of the bed, the flow resistance exhibited by the bed material, and the fluid flow rate. It is generally desirable to minimize this pressure differential and/or increase the fluid flow rate without significantly increasing the required pressure differential. For this reason, a replacement arrangement (radial flow) is sometimes adopted. Therefore, the particulate catalyst J is also shaped into a parameter defined by a member that allows the flow of the catalyst into the catalyst (as the reaction is straightened, the working fluid is radially flowed through the inlet region around the periphery of the cross section of the reactor). The catalyst bed enters the centrally disposed outlet region, or flows in the opposite direction, ie, radially outward from the central inlet region through the catalyst bed, to the outlet or to the collection region disposed at the periphery of the reactor. Radial and axial directions are also possible The flow is used in combination. Although such a radial flow arrangement gives the desired differential pressure advantage, allowing the working fluid to flow at the desired rate, it requires a more complex reactor interior, allowing the particulate catalyst to be added and the -4- paper scale to be applied to Chinese national standards ( CNS)A4 specification (210 X 297 mm) ----------Install-----r--^丨定*-------- (Please read the notes on the back first) Fill in this page again) 1271217 Α7 Β7 V. Description of invention (2) / or inconvenience of unloading. We have designed a device in which the color of the salt, the uranium, or the axial-radial flow can be obtained. 'There is no internal reaction to the complex reaction. So 'this hair Provided is a catalytic reactor having an inlet and an outlet and a bed of catalyst catalyst, the catalyst bed being disposed around a central region communicating with a port and exhibiting a smaller flow resistance than the catalyst particles, the central region of the bed being at least with the catalyst bed The main portion is of equal height. For a catalyst bed of at least a majority of the height, the outer surface of the catalyst bed has a smaller cross section than the reactor, thereby leaving a space on the outer surface of the catalyst bed and the inner surface of the reactor. The catalyst particles show a smaller flow resistance of the particulate material. The catalyst bed preferably has a surface that is close to a single cylindrical or frustum-shaped surface. - face 'or have one or more cylinders and one or more frustum stacked shapes · * one by one ' " a ..., Ministry of Economic Affairs Intellectual Property Bureau employees consumer cooperatives printed external surface. The catalyst bed may have an outer diameter equal to the inner diameter of the reactor, i.e., the portion has no space between the inner wall of the reactor and the outer surface of the catalyst bed. The minimum outer diameter of the surface is smaller than the inner diameter of the reactor such that at least a portion of the height bed has a space between the inner wall of the reactor and the outer surface of the catalyst bed. The two particles exhibit a smaller impedance working fluid flow than the catalyst particles. Similarly, the central region of the catalyst bed preferably has a shape close to a cone, a frustum or a cylinder, or has a shape of a cone and one or more frustum or cylindrical stacks or has one or more different maximum diameters. The shape of a cylinder or frustum is stacked, or has the shape of one or more cylinders and one or more frustums. -5- This paper scale applies to the Chinese National Standard (CNS) A4 specification (210 X 297 mm) 1271217 A7 B7 Ministry of Economic Affairs Intellectual Property Office Staff Consumer Cooperative Printed 5, Invention Description (3 preferably has a shape close to a single cylinder or frustum, preferably with a surface area greater than the cross section of the reactor. The height of the central region of the catalyst bed is predominantly the majority of the catalyst bed, preferably at least 7 〇 〇/〇 of the catalyst bed. The invention is illustrated by the accompanying drawings in which: Figure 1 is a cross-sectional view of an axial/radial flow through a reactor in accordance with the present invention. Figure 2 is a view similar to another embodiment of Figure 1. Figures 3 through 5 are partial cross-sectional views of the fractionation reactor of Figure 1 illustrating the sequence of addition of particulate material to the reactor. Figure 6 is a view similar to another embodiment of Figure 1. In Fig. 1, a reactor 1 having a cylindrical section is shown, which has an inlet 2' at its upper end and an outlet 3 at its lower end. A catalyst limiting perforating device 4 (e.g., a cylindrical wire cage) is disposed above the outlet 3 to define a free space 5 forming a necessary central region within the catalyst bed that communicates with the outlet 3. Around the catalyst limiting device 4 is a bed of particulate catalyst, such as cylindrical particles. The catalyst particles have a maximum and minimum size in the range of 1 to 10 mm and a aspect ratio (maximum size/minimum size) in the range of 1 to 5. The pore size of the catalyst limiting device should be such that the catalyst particles cannot pass. The inner wall 7 of the reactor crucible and the outer surface of the catalyst bed form a zone 8 which is filled with a flow resistance material which is substantially smaller than the particles of the catalyst bed 6. The particulate material of the fill region 8 generally has a particle size greater than that of the catalyst particles. The minimum size of such particles is generally 55 times the minimum size of the catalyst particles, and the maximum size is preferably not more than 2.5 times the maximum size of the catalyst particles. These larger particles may be of a cylindrical configuration or may have one or more axially extending through holes to reduce the working fluid ------------------ (Please read the notes on the back and fill out this page) Φ -6 1271217 Intellectual Property Intelligence Bureau JL Consumer Cooperative Printed A7 B7 V. Invention Description (4) Flow resistance through Zone 8. The particles of zone 8 can also be extended to the top 9 of the catalyst bed. In use, the working fluid is sent to the inlet 2, flows axially downward through the zone 8, and then enters the free space 5 through the catalyst bed 6, thereby reaching the outlet 3. Since zone 8 shows a flow resistance that is less than the flow resistance of catalyst bed 6, the working fluid flows downwardly through zone 8 and then radially through catalyst bed 6 to reach free space 5. At the same time, the working fluid also flows axially downward through a portion of the catalyst bed above the upper portion of the catalyst limiting device 4. If the top of the catalyst limiting device 4 is made of a solid, the catalyst bed above the top of the catalyst limiting device 4 can be omitted, allowing the working fluid passing through the catalyst bed 6 to flow substantially radially. Alternatively, regardless of whether the top of the catalyst limiting device 4 is solid, a disc or plate is placed on top of the deuterating agent bed to change the flow pattern through the upper portion of the catalyst bed. In the specific embodiment of Figure 2 The catalyst limiting device 4 is fabricated in the form of a frustum, which is also a conventional taper configuration. This arrangement results in a more uniform flow distribution of the working fluid through the catalyst bed 6. Preferably, the catalyst limiting device 4 is arranged to pass the working fluid through the catalyst. The flow resistance of the bed is substantially uniform. Figures 3 to 5 illustrate a method of filling a particulate material into a reactor. As shown in Figure 3, a ring 1 is placed in the lower wall 1 of the reactor, preferably at this position in bed 6 and An interface is formed between the regions 8, and the catalyst particles are then filled into the annular region surrounded by the catalyst p-clamping device 4 and the ring 10. As shown in Figure 4, the ring 10 and the reactor are filled with the particles required for the region 8. The annular area between the walls 7. As shown in Figure 5, lift the ring 10 and place it on top of the previously filled particles. Repeat the above paper size for the Chinese National Standard (CNS) A4 specification (210 X 297 mm) -- ------ ---Installation - (Please read the notes on the back and fill out this page) Order · Printed by the Ministry of Economic Affairs, Intellectual Property Bureau, Staff Consumer Cooperatives Α271217
五、發明說明（5) 步碟。應瞭解，當環1 0自床6和區域8之顆粒間提出時， 將有一些顆粒下沈，以填充由環佔據之空間。重複該步 驟’直至將反應器填充至理想高度。 催化劑一般通過反應器上壁之人孔（未示出）加入。爲能 夠將環1 0插入反應器，較佳以能夠通過人孔介入且於反應 咨内裝配之片段製造’和/或由柔動性材料製造，如適合 材料條帶（如塑性材料），其末端固定在一起，形成環形 環。在由柔勃材料末端固定形成環之臺錐形布置中（像是 圖2中所示），形成催化劑區域6之連續層外徑可由改變固 定條帶端之位置減小。同樣，如果根據本發明改變習用轴 向流反應器，催化劑限制裝置4亦較佳爲如此大小和/或分 區限制，以能夠通過入口進入反應器。 亦應瞭解，另一個替代性具體實施例中，可省略催化劑 限制裝置4 (如，線網籠），用低流阻顆粒材料（如，用於區 域8之材料）填充中心自由空間。此時需要沿出口 3布置限 制柵。可用類似於上述對床6和區域8填充材料之方法加入 填充中心區域之顆粒。 在另一種填充反應器之方法中，界定床6和區域8間理想 邊界之柔勃網通過人孔介入，在不移除篩網下用各種材料 填充床6和區域8。此時，該篩網所用材料應能夠經受反應 器隨後使用期間佔優勢之條件，或者在使用降解之分解產 物不得有礙於催化劑或工作流體。可在多種情形下使用由 塑料製造之篩網，如聚丙晞。 因此，本發明亦提供一種用顆粒催化劑床填充具入口和 -8 - (請先閱讀背面之注意事項再填寫本頁)Fifth, the invention description (5) step disc. It will be appreciated that when the ring 10 is raised between the particles of the bed 6 and the zone 8, there will be some particles sinking to fill the space occupied by the ring. This step is repeated ' until the reactor is filled to the desired height. The catalyst is typically added through a manhole (not shown) in the upper wall of the reactor. In order to be able to insert the ring 10 into the reactor, it is preferably manufactured and/or made of a flexible material, such as a strip of material (such as a plastic material), which is capable of being inserted through a manhole and assembled in a reaction protocol. The ends are fixed together to form an annular ring. In a tapered arrangement of the ring formed by the end of the flex material (as shown in Figure 2), the continuous layer outer diameter forming the catalyst region 6 can be reduced by changing the position of the fixed strip end. Similarly, if the conventional axial flow reactor is modified in accordance with the present invention, the catalyst limiting device 4 is also preferably so sized and/or partitioned to be able to enter the reactor through the inlet. It will also be appreciated that in another alternative embodiment, the catalyst limiting device 4 (e.g., wire cage) may be omitted and the central free space may be filled with a low flow resistant particulate material (e.g., material for region 8). At this time, it is necessary to arrange a limiting grid along the outlet 3. The particles filling the central region may be added in a manner similar to that described above for the bed 6 and zone 8 filling materials. In another method of filling the reactor, a soft web defining the desired boundary between bed 6 and zone 8 is interposed by a manhole, and bed 6 and zone 8 are filled with various materials without removing the screen. At this point, the material used in the screen should be able to withstand the conditions prevailing during subsequent use of the reactor, or the decomposition products used in the degradation must not interfere with the catalyst or working fluid. Screens made of plastic, such as polypropylene, can be used in a variety of situations. Therefore, the present invention also provides a filling device with a granular catalyst bed and -8 - (please read the back of the note first and then fill out this page)
A7 1271217 B7 _ 五、發明說明（6 ) (請先閱讀背面之注意事項再填寫本頁) 出口之反應益之方法，其包括，提供於所需催化劑床内界 定中心區域之第一催化劑限制穿孔裝置，且與一個口相 連，在該第一催化劑限制裝置和該反應器内壁之間布置第 二顆粒限制裝置’用顆粒催化劑填充該第一和第二限制裝 置間之空間’用顯示低於該催化劑顆粒流阻之顆粒材料填 充第二限制裝置和反應器内壁間之空間。 可用已知方法將自床6和區域8之顆粒自反應器卸出，例 如，在反應器下壁提供卸料口、和/或通過人孔或用於裝 料之其它孔插入軟管，通過軟管眞空抽取。如果床6和區 域8所用之顆粒大小芫全不同，若需要，可將經卸出催化 劑過篩’使區域8之較大顆粒自催化劑顆粒分離。 在圖6所示之具體實施例中，中心管1 2入口 2連接，該 管之較下部分1 3具有穿孔，並伸入催化劑床6，如此界定 催化劑床6内之中心區域。在該具體實施例中，催化劑床 在錐臺1 5頂部具有圓柱1 4形之外表面，該錐臺1 5在其下 經濟部智慧財產局員工消費合作社印製 取小直么’而在圖2之具體貫施例中，最小直徑位於上 端。在圖6之具體實施例中，圓柱形部分1 4具有與反應器 内徑相同之直徑，但深度僅爲催化劑床6深度之一小部 分。催化劑床6外表面之錐臺部分1 5和反應器内壁7以及 催化劑床6下端1 6和出口 3間之空間8用顯示小於催化劑顆 粒流阻之顆粒材料填充。 使用時，工作流體通過入口 2送入，向下通過管1 2，且 通過其間之穿孔流出。工作流體因而徑向向外流動通過催 化劑床’進入催化劑床臺錐部分外表面和反應器内壁間之 • 9 · 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297i釐)~ 1271217 A7 B7 經濟部智慧財產局員工消費合作社印製 五、發明說明（7 ) 空間8，達到出口部分3 [此處提供栅（板）（未顯示），以防 止填充空間8之顆粒材料進入出口 3]。由於管12在高於催 化劑床6之上表面部分有一些穿孔，工作流體可自管1 2流 入高於催化劑床6之空間，軸向向下通過催化劑床之上部 圓柱形部分1 4，進入區域8。 可用上述圖3至5之類似方法形成相鄰床顆粒催化劑以及 填充催化劑外表面和反應器内壁間之空間8之顆粒材料， 但在介入限制裝置以界定區域8和催化劑床在錐形壁之邊 界之前，用顯示較小流阻之顆粒填充反應器下端，以在催 化劑床6之底部1 6和出口 3之間提供該種材料層。 在另一個具體實施例中應瞭解，用於填充區域8 (和/或 區域5，如果用顆粒材料填充）之顆粒可爲顆粒催化劑，但 其大小或構型應使該顆粒流阻小於催化劑床6顆粒之流 阻。 本發明特別用於將先前用於軸向流方式之反應器轉化爲 軸向/徑向或徑向流，而不用使反應器發生重大内部改 變0 因此，我們亦提供一種將具入口、出口和人孔之反應器 自軸向流方式轉化爲軸向/徑向流或徑向流方式之方法， 其包括，通過該人孔送入催化劑限制穿孔裝置，將該催化 劑限制裝置附著至一個口，以對該部分長度反應器自該口 延伸界定包圍物，將顆粒催化劑材料裝入反應器，以圍繞 該催化劑限制裝置建立催化劑床，且對該床之至少部分高 度而言，將比該催化劑顆粒顯示更小流阻之顆粒材料加至 -10 - 本紙張尺度適用中國國家標準<CNS)A4規格（210 X 297公釐） ---------------r--Γ I ^ -----I I I I I (請先閱讀背面之注意事項再填寫本頁) 1271217 經濟部智慧財產局員工消費合作社印製 A7 B7 五、發明說明（8 ) 該床外表面和反應器内壁間之區域。 本發明可用於任何固定床催化製程，特別用於包含氣態 工作流體絕熱反應之製程。此類反應之實例爲低溫絕熱蒸 氣轉化反應、水煤氣轉換反應、甲醇合成反應、甲烷化反 應、氨合成反應及氫化反應。 因此，本發明進一步提供一種方法，其包括使工作流體 通過反應器入口，然後通過該反應器内之一系列區域，最 後通過該反應器出口，其中該第二區域爲於形成第一和第 三區域之一之中心區域周圍布置之固定催化劑床，該第二 區域與一個口相連，並顯示比該催化劑床更小對工作流體 之流阻，該中心區域具有等於該床主要部分高度之高度， 對至少主要部分催化劑床高度而言，該催化劑床之外表面 具有小於反應器之截面，因而在催化劑床外表面和反應器 内壁之間留下空間，該空間用比催化劑顆粒展現更小流阻 之顆粒材料填充，並形成該第一和第三區域之其它部分。 作爲實例，我們將本發明圖2所示之反應器與習用軸向 流反應器用氧化鐵/氧化鉻顆粒催化劑之高溫轉移反應器 進行比較。 習用軸向流反應器具有3 . 7米内徑，其凹曲下端（對應於 圖2之區域D e )具有〇·93米高度（距離D E )。催化劑限制柵 圍繞出口布置。凹曲下端用對工作氣流顯示較小阻力之惰 性氧化鋁球填充。反應器之圓柱形部分（對應於區域A D ) 用4 0禾）圓柱形催化劑顆粒（直徑$ 5毫米，長4 · 9毫米）填 充。催化劑床之高度爲3 . 7米，即距離A D。在催化劑床頂 -11 - 本紙張尺度適用中國國家標準（CNS)A4規格（210 x 297公釐） ^1 ---------· — — — — ——— (請先閱讀背面之注意事項再填寫本頁) 1271217A7 1271217 B7 _ V. INSTRUCTIONS (6) (Please read the note on the back and then fill out this page.) The method of export benefit includes the first catalyst-limited perforation provided in the desired catalyst bed defining the central region. a device, and connected to a port, between the first catalyst limiting device and the inner wall of the reactor, a second particle restricting device is disposed to fill a space between the first and second restricting devices with a particulate catalyst. The particulate material of the catalyst particle flow resistance fills the space between the second restriction device and the inner wall of the reactor. The particles from bed 6 and zone 8 can be discharged from the reactor by known methods, for example, by providing a discharge port on the lower wall of the reactor, and/or by inserting a hose through a manhole or other hole for charging. The hose is hollowed out. If the particle size used in bed 6 and zone 8 is different, if desired, the catalyst can be sifted to remove the larger particles of zone 8 from the catalyst particles. In the particular embodiment illustrated in Figure 6, the central tube 12 inlet 2 is joined, and the lower portion 13 of the tube has perforations and extends into the catalyst bed 6, thus defining a central region within the catalyst bed 6. In this embodiment, the catalyst bed has a cylindrical outer surface on the top of the frustum 15 and the frustum 15 is printed on the lower part of the Ministry of Economic Affairs, the Intellectual Property Bureau, and the consumer consortium. In the specific embodiment of 2, the minimum diameter is at the upper end. In the particular embodiment of Figure 6, the cylindrical portion 14 has the same diameter as the inner diameter of the reactor but is only a fraction of the depth of the catalyst bed 6. The frustum portion 15 of the outer surface of the catalyst bed 6 and the inner wall 7 of the reactor and the space 8 between the lower end 16 of the catalyst bed 6 and the outlet 3 are filled with a particulate material which exhibits a flow resistance smaller than that of the catalyst particles. In use, the working fluid is fed through the inlet 2, down through the tube 12, and exits through the perforations therebetween. The working fluid thus flows radially outward through the catalyst bed 'between the outer surface of the catalyst bed cone portion and the inner wall of the reactor. · 9 · This paper scale applies to the Chinese National Standard (CNS) A4 specification (210 X 297i PCT) ~ 1271217 A7 B7 Ministry of Economic Affairs Intellectual Property Bureau employee consumption cooperative printing 5, invention description (7) space 8, reaching the exit part 3 [here a grid (plate) (not shown) to prevent the filling of the granular material of the space 8 into the exit 3] . Since the tube 12 has some perforations in the upper surface portion above the catalyst bed 6, the working fluid can flow from the tube 12 into the space above the catalyst bed 6, axially downward through the cylindrical portion of the upper portion of the catalyst bed, into the region. 8. The adjacent bed particle catalyst and the particulate material filling the space 8 between the outer surface of the catalyst and the inner wall of the reactor may be formed by a similar method as described above with reference to Figures 3 to 5, but with the intervention limiting means to define the region 8 and the catalyst bed at the boundary of the tapered wall. Previously, the lower end of the reactor was filled with particles showing a smaller flow resistance to provide this layer of material between the bottom 16 of the catalyst bed 6 and the outlet 3. In another embodiment, it will be appreciated that the particles used to fill region 8 (and/or region 5 if filled with particulate material) may be particulate catalysts, but may be sized or configured such that the particle flow resistance is less than the catalyst bed. 6 flow resistance of the particles. The invention is particularly useful for converting a reactor previously used in an axial flow mode to an axial/radial or radial flow without significant internal changes to the reactor. Thus, we also provide an inlet, an outlet, and A method for converting a manhole reactor from an axial flow mode to an axial/radial flow or a radial flow mode, comprising: feeding a catalyst limiting perforation device through the manhole, attaching the catalyst restriction device to a port, Extending the enclosure from the port by the length of the reactor, loading the particulate catalyst material into the reactor to establish a catalyst bed around the catalyst limiting device, and at least a portion of the height of the bed will be compared to the catalyst particles Adding a smaller flow resistance to the particulate material to -10 - This paper scale applies to the Chinese National Standard <CNS) A4 specification (210 X 297 mm) ---------------r- -Γ I ^ -----IIIII (Please read the note on the back and fill out this page) 1271217 Ministry of Economic Affairs Intellectual Property Office Staff Consumer Cooperative Printed A7 B7 V. Invention Description (8) The outer surface of the bed and the reactor The area between the inner walls. The invention can be used in any fixed bed catalytic process, particularly in processes involving adiabatic reactions of gaseous working fluids. Examples of such reactions are low temperature adiabatic steam reforming, water gas shifting reaction, methanol synthesis reaction, methanation reaction, ammonia synthesis reaction, and hydrogenation reaction. Accordingly, the present invention further provides a method comprising passing a working fluid through a reactor inlet, then through a series of zones within the reactor, and finally through the reactor outlet, wherein the second zone is for forming first and third a fixed catalyst bed disposed around a central region of one of the regions, the second region being coupled to a port and exhibiting a smaller flow resistance to the working fluid than the catalyst bed, the central region having a height equal to the height of the main portion of the bed, For at least a major portion of the catalyst bed height, the outer surface of the catalyst bed has a smaller cross-section than the reactor, thereby leaving a space between the outer surface of the catalyst bed and the inner wall of the reactor which exhibits a smaller flow resistance than the catalyst particles. The particulate material is filled and forms other portions of the first and third regions. As an example, we compare the reactor of Figure 2 of the present invention with a conventional high temperature shift reactor for an axial flow reactor using an iron oxide/chromia oxide catalyst. The conventional axial flow reactor has an inner diameter of 3.7 m, and its concave curved lower end (corresponding to the region D e of Fig. 2) has a height of 93 m (distance D E ). The catalyst confinement grid is disposed around the outlet. The lower end of the concave curved portion is filled with an inert alumina ball which exhibits less resistance to the working air flow. The cylindrical portion of the reactor (corresponding to the region A D ) was filled with cylindrical catalyst particles (diameter: 5 mm, length 4 · 9 mm). The height of the catalyst bed is 3.7 meters, which is the distance A D . At the catalyst bed top -11 - this paper scale applies the Chinese National Standard (CNS) A4 specification (210 x 297 mm) ^1 ---------· — — — — — — (Please read the back first Note on this page again) 1271217
經濟部智慧財產局員工消費合作社印製 邵填充1 5 0毫米深度氧化鋁球層。 一使用時，含56.5莫耳％氫氣、129莫耳％一氧化碳” $ ::/〇一虱化碳、〇.3莫耳％甲烷和228莫耳％氮氣之氣體 占物以υο,οοο標準立方米/小時速率與75,〇〇〇標準立方 米/小時水瘵汽以鬲壓通過催化劑床。通過該催化劑床之 壓降約爲0.25巴（bar)。 士根據本發明，用圖2所示之裝置修改以上軸向流布置。 至錐形篩網4兩側邊傾斜，與水平線成8〇。角。該錐臺高 於線〇之高度（即距離CD)爲2 8米，於線D之直徑爲^^ =，於線C處之直徑爲0.52米。將催化劑裝入反應器，以 塡充下部凹曲端之空間（代替氧化鋁球），然後作爲錐臺装 至線B。該錐臺同樣具有與水平成8 〇。角之側邊。距離 B D爲3 · 7米。催化劑床於線d處爲之外徑3 . 7米，即反應 器整個内徑。催化劑床外之空間用具1 〇毫米直徑中心孔之 1 7爱米直徑和1 7毫米高度之氧化鋁環填充。此等環層亦 布置成高於催化劑頂部i 5 〇亳米高度（即，距離Ab )。催 化劑之總體積爲3 3米3。由於軸向流布置使用4 〇米3催化 劑’爲補償催化劑體積減小，可使用較小催化劑顆粒大 小。因此，該催化劑顆粒爲5 · 4毫米直徑和3 . 6毫米長度之 圓柱形顆粒。因爲該催化劑顆粒每單位體積具更高幾何表 面積，所以該較小顆粒每單位體積具更大活度。3 3米3該 較小顆粒約等於4 0米3習用轴向流布置所用較大顆粒之催 化效能。 计算表明’在習用軸向流布置之相同條件下，本發明布 置之壓降爲0.13巴。 -12- 本紙張尺度適用中國國家標準（CNS)A4規格（210 x 297公釐） 一 ^----— --- ----I — — — · I I I l· I I ^ ·1111111 {請先閱讀背面之、注音？事項再填寫本頁)Printed by the Ministry of Economic Affairs, the Intellectual Property Bureau, the Consumer Cooperative, Shao filled with a 150 mm deep alumina sphere. When used, it contains 56.5 mol% hydrogen, 129 mol% carbon monoxide": ::/〇 虱 carbon, 〇.3 mol% methane and 228 mol% nitrogen gas υο, οοο standard cube The meter/hour rate is 75, 〇〇〇 standard cubic meters per hour of water vapor is passed through the catalyst bed by pressure. The pressure drop across the catalyst bed is about 0.25 bar. According to the invention, as shown in Figure 2 The device modifies the above axial flow arrangement. The sides of the tapered screen 4 are inclined at an angle of 8 〇 to the horizontal line. The height of the frustum is higher than the height of the turns (ie, the distance CD) is 28 meters, on line D. The diameter is ^^ =, and the diameter at line C is 0.52 m. The catalyst is charged into the reactor to fill the space of the lower concave end (instead of the alumina ball), and then mounted as a frustum to the line B. The frustum also has a side with an angle of 8 〇. The distance BD is 3.7 m. The outer diameter of the catalyst bed at line d is 3.7 m, which is the entire inner diameter of the reactor. 1 Amm diameter and 1 7 mm height of the alumina ring filling of the 1 mm diameter center hole. These ring layers are also arranged higher than The top of the chemical agent i 5 〇亳 height (ie, distance Ab). The total volume of the catalyst is 33 MPa. 3. Because the axial flow arrangement uses 4 〇 3 catalyst 'to compensate for the catalyst volume reduction, a smaller catalyst can be used. The particle size. Therefore, the catalyst particles are cylindrical particles having a diameter of 5.4 mm and a length of 3.6 mm. Since the catalyst particles have a higher geometric surface area per unit volume, the smaller particles have a larger life per unit volume. Degree of 3 3 m 3 The smaller particles are approximately equal to the catalytic performance of the larger particles used in the conventional axial flow arrangement of 40 m. The calculations show that the pressure drop of the arrangement of the present invention is the same under the same conditions of the conventional axial flow arrangement. 0.13 bar. -12- This paper scale applies to the Chinese National Standard (CNS) A4 specification (210 x 297 mm). One ^----- ---- ----I — — — · III l· II ^ · 1111111 {Please read the back, phonetic? Please fill out this page again)